Process for producing acetylene and lime hydrate



June 11, 1940. H. v. KoJoLA Er AL 2,204,184

rnocnss von rnonuome ACETYLENE AND mm Hmmm Filed Inch 27, 195e 2 sheets-sheet 1 56 ref` l 4\ il i INVENTORS HUGO lf. KOJ'OLA ATTO RN EY June 11, 1940. H v KOJQLA ET AL) 2,204,184

PRocEss Fon rnonucma ACETYLENE AND LIME HYDRATE Filed'larcn 27, 195e 2 sheets-sheet z INVENTORS HUGO KOJ'OLA MAUR/CE O'BR/AN ATTO R N EY Patented June 11, 1940 .UNITED STATES PATENT OFFICE PMCESS FOR PRODUCIN G ACETYLENE AND LIME HYDBATE lingo V. Koiola and Maurice OBrian, Indianapolis, Ind., asslgnors to The Prest-O-Lite Company, Inc., a corporation of New York Application March 27, 1936, Serial No. 71,2i

Claims.

This invention relates tothe generation of a Sas wherein the gas is produced by the reaction of a solid and a liquid. More specifically, this invention relates to the generation of acetylene 5 by the reaction of the calcium carbide and water,

and particularly to the simultaneous production of acetylene and a substantially. dry residue of l calcium hydrate. This latter process is known as dry generation.

The reaction which takes place when calcium carbide and water are brought together is represented by the following:

Prior to the advent of the dry generation of acetylene it was customary to generate acetylene by droppins granular calcium carbide into a body of water contained in a generating chamber. Seven to ten times the amount of water necessary to-y complete the reaction was used so as to utilize the heat carrying capacity of the excess of vwater to absorb the heat of reaction, since the reaction ls highly exothermic. The principal disadvantage incurred in this method of generation was 25 the production of the calcium hydrate as a lime sludge. This sludge was cumbersome to handle and ditlicult to dispose of since the calcium hydrate could be recovered in a dry and useable form only at considerable expense.

In an attempt to obviate this difliculty the process of dry generation was developed. In

this 4process the calcium carbide is contacted with an amount of water limited to that necessary to completely react the carbide, plus an additional amount which is evaporated so as to utilize the latent heat of evaporation of the excess water to absorb the heat of reaction. While this process should produce a substantially dry residue, the acetylene evolved is saturated with water vapor v by the evaporation of the excess water supplied for the purpose of limiting the maximum temperature reached to a temperature of 100 C. or lower. By limiting the temperature to a value below 100 C., there is a tendency for the moisture 5 in the saturated acetylene to condense ,upon

the dry. residue when cooled, and thus defeat the very purpose of the dry generation.

' `Since the water used in the generation of acetyiene almost invariably carries Jimpurities in the 56' form of dissolved gases such as air, any excess water used in the generation of acetylene will increase'the amount of those impurities. The presence of these impurities is especially disadvantageous in acetylene to be utilised in chemical in be com and forced into cylinders containing acetonev for the purposev of dissolving the acetylene. In chemical systems the presence of these impurities and their accumulation will necessitate periodic blowoffs, which obviously interrupt the, cycle and 5 cause the loss of gas. In acetylene used for compression into cylinders containing acetone and a porous filler, the presence of impurities will cause the pressure to build up abnormally because such impurities are much less soluble in acetone than acetylene. A decrease in the amount of impurities will increase the amount of acetylene thati can be dissolved in a cylinder without exceeding a desired pressure limit.

Broadly, the main object of this invention is u to provide an improved method of producing a lgas and a substantially dry residue by the reaction of a solid and a liquid; and, more specilically, to provide a method of producing acetylene and substantially dry calcium hydrate by the reaction of calcium carbide and water, such method being adapted to produce the acetylene and the dry calcium hydrate at temperatures substantially in excess of 100 C., thereby rendering the gas substantially free from impurities. Other objects of this invention are to provide an improved method of producing a gas and a substantially dry residue by the reaction of a solid and a liquid, which will be continuous, simple and efficient; to

provide such methods wherein the temperature in y of a modified form of gas generating apparatus;

Fig. 4 is a fragmentary vertical sectional view of the apparatus shown in Fig. 3,.the view being taken substantially along the line 4-4 of Fig. 3:

and A Y Fig. 5 is a view similar to Fig. 4 and illustrating a modified position for introducing the water o into the generating chamber.

It has been found that with maximum temperatures occurring up to-400 C. acetylene, substantially free from impurities, can be safely generated in large quantities by the reaction of calcium carbide with a limited amount of water, if the carbide and hydrate produced are kept in constant agitation and the proper amount of water is added at a plurality of points along a predetermined path in a generating chamber. At temperatures above 400 C., the decomposition of acetylene occurs. In addition, it has been found advantageous to remove the generated acetylene as promptly'as possible so that the time of contact of the acetylene with the reacting portions ofthe carbide will be limited. By controlling the quanf tity of water supplied to only a slight excess over vthat theoretically required to complete the reaction (the exact amount depending upon the rate and temperature of generation in relation to the various features of the apparatus employed),

a residue of substantially dry hydrated lime and acetylene gas having a considerably decreased moisture content may be continuously produced. i

An apparatus for carrying out the reaction according to the invention comprises xed horizontal tubular chambers arranged in single or multiple units according to the working space available and provided with agitator paddle conveyor means disposed longitudinally within each chamber, the u construction of said conveyor means being such that the generated'gas may have a substantially unim-peded iiow out of the chamber. Carbide from one or more feed hoppers is supplied to the first reaction chamber by a suitable means and the water is introduced at desired points in the reaction chamber along the path of the carbide. A sufiicient length of reaction chamber and mixing conveyor is provided to insure complete conversion of the carbide into a residue of substantially dry hydrated lime which may be discharged into a lime hopper. The gas after generation is preferably passed through dust separating means and a cooler.

Briefly, the apparatus shown in Fig. 1 consists of a vertical carbide supply hopper I3 disposed above a second vertical hopper I which is adapted to discharge carbide into an upper horizontal reaction chamber 36 at predetermined rates by means of a feed screw I9. A plurality of spaced rotatable paddles 35 mounted on an axially disposed shaft 21 are arranged to sweep the entire inner surface of the chamber, and adapted to continuously mix and convey the carbide to a vertically disposed passage 38 between the upper reaction chamber 36 and a lower horizontal reaction chamber 31. In the lower reaction chamber spaced paddles 35a are provided on a shaft 21a as in therupper reaction chamber. Water may be introduced into the reaction chambers by spray nozzles 41 and the dry hydrate discharged into a lime hopper 33 through a vertical -conduit 3l connected to the lower reaction chamber 37 at its discharge end. The generated gas is .adapted to pass through pipe 56 into a separator 5I and thence into a cooler 56.

In detail it will be seen that the upper carbide supply hopper I3 is provided with an air-tight door II which is adapted to be closed by clamp I2, and a valve i4 to control communication with the lower hopper I5. The lower hopper I5 is connected to the feed conduit I1 by a passage controlled by valve I6. In the feed conduit I1 there is provided a feed screw I9 carried by a shaft I8 which 'extends through the hopper end of the feed conduit and is Joumaled in bearings 20 and 20a positioned in the ends of the feed conduit. A suitable air-tight packing, which is not shown, is preferably provided at bearing 20. The feed conduit I1 communicates with the upper reaction chamber 36 through passage 2|. Shafts 21 and 21a carrying blades or paddles 35 and 35a are centrally located in the upper and lower reaction chambers and are journaled in bearings 30 and 39 provided in the ends of said chambers. An air-tight packing, also not shown, which may be similar to the one provided at bearing 20, is preferably provided at each of the bearings 30. The drive for the shafts I8, 21, and 21a comprises a motor M driving reduction-gearing R connected to a shaft 24 on which is mounted a sprocket wheel 23 and a pinion 25. The sprocket 23 drives the shaft I8 through a chain 22 carried upon it and upon a sprocket 23a` on the shaft I8. The pinion 25 drives shafts' 21 and 21a through gears 26 and 26a which intermesh therewith.

When the paddles 35 are turned by the shaft 21, they are adapted to continuously agitate, mix and convey the carbide through the length of the upper reaction chamber 36 to the passage'38 which communicates with the lower reaction chamber. The paddles 35a are likewise adapted to agitate and convey the reacting carbide and calcium hydrate through the length of the lower reaction chamber 31 to the discharge conduit 3I which is connected to the discharge hopper 33 and iscontrolled by a valve 32. The discharge hopper 33 is adapted to receive and temporarily hold the dry lime hydrate, and a valve 34 is provided at the bottom of the discharge hopper to permit removal of the dry hydrate, from time to time as desired.

The water to contact the carbide is supplied through a main supply line 4I in which is placed a control valve 40, a metering orifice 42 and a ilow meter 43 actuated by the pressure drop of the fluid passing through the orifice. The upper and lower reaction chambers are served by supply pipes 44 and 45 respectively, which lead from the main line ,4I. The water is introduced into the reaction chambers from the supply pipes 44 and 45 by means of a plurality of branches 48 which enter the reaction chambers and are adapted to discharge the water therein through a plurality of nozzles 41. The supply of water to each nozzle is controlled by a valve 46 placed in its respective branch 48.

The generated gas or acetylene passes into the centrally located collecting conduits 49 shown more clearly in Fig. 2, and into the main header 50. Thence it passes into a .dust separating device or chamber 5I provided at its lower end with a valve 52 and adapted to remove and hold small -particles of the dry hydrate which may be carcooler at a water outlet 60, may be discharged as waste or by-passed into the water supply line 4I.

A pipe 66-leading from. the gas holder is connected to the upper and lower carbide hoppers and the upper generating chamber through mined rate by the position.

branches 31, vacuum relief 88, 10, and 1I respectively. filled -to pending pipe .61 with water or other suitable liquid. If a vacuum occurs in either of the hoppers or in the generating chambers upon shutdown of the apparatus, the acetylene will ilow back from the gas holder through the pipe 38 and seals 68.

The operation of the apparatus of Figs. 1 and 2 is as follows: At the start, the valve I4 between the upper and lower carbide hoppers is opened, the clamp I2 is un'fastened and the-air-tight lid II of the supply hopper I3 is swung to an open Carbide is introduced into the supply hopper and passes into the lower hopper I 5 through the open valve I4. When both hoppers are full, the air-tight lid II is clod and clamp I2 tightened down, and the carbide is ready to be fed into the generator. the operation of the apparatus when' the supply hopper needs to be refilled, the valve I 4 is tightly closed, the air-tight lid I I is opened as before, and the hopper I3 is lled with carbide. Upon closing and clamping the air-tight lid II, the depleted carbide in the lower hopper I5 may be replaced by opening the valve I 4 to permit the fresh carbide to pass from the upper hopper to the lower hopper. The supply hopper may thus be, refllled while at all times excluding admission of air to or loss of gas from the generating chamber by the use oi' the double valvesystem provided by lid II land valve Il.

Before beginning the feed of carbide it is preferable that the reaction chambers and other gas spaces be purged of a'irby the introduction of acetylene from a convenient source. To feed the carbide into the generating chambersthe motor M is started, which will cause the shafts I 3, 21, and 21a to rotate, which in turn will cause gtatlon of the screw I9 and the paddles 35 and a. valves It and 32 are then opened, and the hydrate removal valve 3l closed. 'I'he carbide from the lower hopper will pass into the feed conduit I1 where it will be conveyed at a uniform predeterscrew I9 into the upper reac seals 88, and pipes The seals 33 are tion chamber 36 tion chamber by the paddles 35. To contact the carbide with water the control valve 40 is opened to a degree suillcient to control the rate of through the generating chamber. 'I'he nozzles 41 project the water onto the agitated and moving the water to generate the desired acetylene. As succeeding portions of the carbide are contac acted and unreacted portions of the carbide pass path but it has been from the upper generating chamber into -the lower generating chamber where they will be further contacted with water from the nozzles in that ofunreactedl carbide remaining in the mass may a point above the lower end of the de' may be withdrawn at will the gas holder by means of the The carbide feed and hydrate discharge and conveyed along the reace generator is opera portions `4lthe shafts 21',

33 and 33 correspond to the same-parts in the 3 absorb and react with any waterinadvertently contained in the hydrate. In this way a substantially dry hydrate is conveyed to the discharge conduit 3I from whence it will pass into the hopper 33 through the valve 32. In order to discharge the dry hydrate from the hopper 33 without interfering with the continuous operation of the process, the valve 32 maybe closedthe valve 34 opened, and the hydrate then discharged through the valve 3l, while hydrate produced during the discharge interval will collect in passage II. After the desired amount of collected hydrate has been discharged the valve 34 is closed and the valve 32 opened, so that the accumulated hydrate in passage 3| will pass into the hopper 33, and the normal operation is resumed. l

The continuously generated acetylene passes through headers 49 and main header 50 into a suitable gas cleaning device such as the separator 5I where small particles of hydrate which have been carried over by the acetylene settle to the lower portion of the chamber 5I from which they through the valve 52. When lthe valve 53 is opened, the vgass passes through conduit 54 to the cooler I3, entering the cooler through the gas inlet 55. 'I'he cooling water entering at 51 is distributed through tubes 62 by a header 63, to collect in the header 64 and pass from the cooler at the outlet 60. The passage of the water cools the tubes, and the gas cooled by contact with the outside of the tubes. A set of badles 6I in the cooler serves to direct the gas into contact with all of the tubes. The cool gas passes through the outlet 53 and is led into conduit 59.

As has been shown, the operation of the apparatus is continuous since the carbide supply hopper is adapted to be charged, andthe hydrate hopper is adapted to be discharged, without interfering with the operation of the generator. The amount of water vcontacting the carbide, which is measured so as to excess of that necessary to completely react the carbide introduced, is tregulated by the valve l0 in conjunction with the rate of flow as indicated by the dow meter. In addition, suitable temperature indicating apparatus may be provided at various points along the path of reacting carbide'and the distribution of the water supplied to the several nozzles may be regulated by the valves 48 accordingly so as to achieve the most desirable working conditions.

While any suitable apparatus for eil'ectively agitatlng and moving the mixture of carbide and calcium hydrate may be used in lieu of the paddies 35 and 35a, the paddles are considered advantageous since they have less tendency to interfere with the direct escape of thel generated acetylene from the point of generation to the, space in the top of the generating chamber. This direct flow is advantageous, especially whenI the d under conditions in wlhich the local temperatures approach 400 C., the dissociation temperature of acetylene, for the gas carries oil' a considerable amount of the heat of reaction, and-rapid removal of this heat is seen to be quite desirable.

Another arrangement of the apparatus adapted for the generation of acetylene according to the invention is shown in Figs. 3 and 4, where the upper and lower reaction chambers 36 and 31: 21a, the paddles 3l, 33a, bearings be v only slightly in entering at inlet 55 and flowing in a path sub- `stantially counter to the path of the water is apparatus of Fig. 1. The shaft 21' in this arrangement, however, is provided with an axial f' passage through which acooling medium may be passed when it is desired to remove heat from the contents of the chamber 36 by conduction through the paddles 35 vand the walls of the shaft 21 to the cooling medium.v The means for I water. The supply hoppers and feeding device l including feed conduit I1, shaft I8, and conveying screw I9 adapted to feed the carbide into the upper reaction chamber through conduit 2|, and

the discharge hopper 33 with the discharge conduit 3| and valve 92 also correspond to similar parts in the apparatus of Fig. 1. In the apparatus of Fig. 3, the water is introduced into the reaction chambers on the sides, as shown more clearly in Fig. 4. The branch pipe 48 and valve 46 are provided with an extension |48 which enters the reaction chamber 26 and is afiixed thereto by an air tight weld 86.- 'I'his extension |48 is adapted to discharge the water onto the lower portion of the wall of the generating chamber throughla wide-mouth nozzle portion |41.

In the apparatus of Fig. 3 the acetylene is preferably discharged at a. plurality of points at the top of the reacting chambers by means of collecting conduits |49 similar to the conduits 49 4 of Fig. 2, but .having individual risers |49a which join and conduct gas into a main header |50. From the header |59 the acetylene passes through a valve |52, a conduit III, and to a separator III by meansof inlet 8|. Disposed in the separator isa filter bag 92 made of noniniiammable porous material, such as woven asbestos.A The acetylene is forced to pass through this filter bag and in doing so will deposit the small particles of hydrated lime carried by it upon the inner surfaces of the bag. At periodic intervals the bag is shaken'by means of iilter bag shaking apparatus customarily employed for such purposes but not shown in the interests of clearness of the drawings. This causes the collected hydrate to fall fromthe inside wall of the bag down into a collectlng receptable I3 from which it may be removed at 'periodic intervals, or whenever necessary. Aiter passing through the bag the acetylene passes from the separatorthrough the outlet 94 and into conduit l5 which leads to the inlet Si of the cooler 5G. The cooler Si is similar in all respects to the cooler shown in Fig. 1 and the acetylene enters through the inlet Si and. after being cooled, is discharged through outlet ,il into the conduit S9 which conducts it to theA "gas holder or other collectingv mea The operation of the apparatus shown in Fig. 3 is substantially as follows: 'Ihe carbide is fed into the reaction chamber by the screw Ilzwthe reacted and unreacted portions of carbide are moved and agitated along a path through the reaction chambers 36 and 31, and the hydrate is discharged through the conduit 3| in a manner similar to that employed in the apparatus of Fig. 1.

'I'he carbide, however, is contacted by the water in a manner dierent from that employed in the apparatus of Fig. '1.' As shown in Figs. 3 and 4, the water is fed in desired increments into the side of' the reaction chamber by the. tangentially directed slotted nozzles |41 which pro- Yject the water directly into the moving mass of carbide and hydrate instead of allowing it to fall through the gas onto the carbide. When operation is. carried on at relatively high temperatures this method of contact is quite advantageous since the warm acetylene which is generated by the reaction of the previous portions of water will not pass upthrough the spray and vaporize and carry away a portion of the water intended for use as a reactant and coolant of the solids. In Fig. 4 the height levels which the reacting solids may assume is shown by a broken line 91 andthe nozzle is shown as conducting the water into the reaction chamber on the low side of the carbide, that is on the side of the downward movement of the paddles 35. As succeeding portions of the carbide are reacted, the paddles in agitating and conveying the mixed solids' along -their path through the reaction chamber will break up small accumulations of hydrate that tend to collect near the nozzles and mix them with the reacting mass of solids so that the water is thoroughly distributed. The lighter particles of'hydrate will tend to be carried to the high side of the line 91, since the lumps of unreacted carbide vare heavier and tend to drop back and moveualong the bottom of the reaction chamber. By introducing the water at the side and directing it so that it will iiow down to the vbottom of the reaction chamber the heavier lumps of carbide will be contacted by the water in preference to the lighter and smaller flakes ot dry hydrate. A

It will be seen that the continuous and thorough agitation of the lumps of carbide causes the layers of hydrate that tend to accumulate on the surfaces of the lumps to be continuously removed asthey are formed. This removal allows the water and steam to have more direct contact with the carbide so that although the reaction speed is increased, the loss of heat from the lumps of carbide is greatly increased by lpassage of heat tothe apparatus and to the gas produced, and 'by loss of heat to evaporate water.

The lumps of carbide are thus prevented from attaining excessive local ltemperatures which may cause local decomposition of the acetylene. To further reduce the amount of excess water vfed into the reaction chambers, it may be desirable to cool the chambers, for example by providing cooling water jackets around the chamber Ii and by providing passages'through the paddle shafts for cooling water as shown in Fig. 3. 1

alternative arrangement for introducing the water is shown in Fig. 5, in whichthe branch unreacted -carbide which ow in thev bottom ofl the moving mass of solidsand the added propulsion which the projected water gives to the heavier portions of the moving mass.

An advantage, however. of introducing the water in the side, as in Fig. 4, over its introduction in the bottom, as in Fig. 5, consists in the .stituents which produce No. 305,080, led November 18, 1939.

ner than that with duced until the reaction 4of such liquid at a plurality of points along said diminished tendency of the nozzles I 41 of Fig. 4 to become clogged when a relatively larger amount of water is used, since the paddles 35 kare always sweeping material away from said nozzles in a much more positive and certain manwhich the paddles 35 push the mass of solids over the nozzle 241.

When saturation with water vapor of the acetylene conducted to the holder is not undesirable, a water-spray scrubbing tower may be used in lieu` of the separator and cooler.

While the operation of the apparatus has been described as continuo it is readily seen that it may be discontinuous, i. e. the generating reaction chambers may be rst filled with carbide and then later contacted with the required amount of water, no more carbide being introof the first portion in. troduced is complete, the process being repeated by successive batches.

While this invention has 'been described as being embodied in a specific form o1' acetylene generator. it will be understood that other conagas by the reaction o! a solid and a liquid may be used in place of carbide and water,-and other gases than acetylene may be produced. It will also be understood that changes `may bemade in the apparatus which will fall within the spirit of this invention. The apparatus described hereinabove and shown in the accompanying drawings forms the subject-matter of our copending application Ser.

What is claimed is: v

1. A process for the continuous and simultaneous production of a gas and a substantially dry residue by the and a liquid, which comprises continuously in troducing said 'solid into a reaction chamber, contacting the solid in said reaction chamber with only suiiicient liquid, in excess of the theo: retical amount necessaryl to completely react the solid, to absorb only that portion o1' the heat oi reaction necessary to maintain the products of reaction at a temperature substantially above the boiling point of said liquid, introducing said liquid directly into said solid to prevent its contacting the generated gas, continuously conveying the unreacted solid and the solid products of reaction along a predetermined path in said reaction chamber, and simultaneously agitating the unreacted sclid and solid products oi reaction so as to completely react the solid, continuously discharging the generated gas from said chamber at predetermined points in the path of said solid and solid products of reaction, and continuously discharging the substantially dry residue from said reaction chamber at the end point of said path.

2. Av process for the continuous and simultaneous production of a gas and a substantially dry residue by the exothermic reaction ot a solid and a liquid, which comprises the steps of introducing such solid into a reaction chamber; initially contacting the solid in said reaction chamber with a portion ot such liquid so as to react a portion of such solid, the amount oi' liquid added being varied in response to the temperature attained by the products of the reaction; introducing said liquid directly into said solid to prevent its contacting the generated gas; conveying and agitating the unreacted solid and solid products o! reaction along a predetermined path in said reaction chamber; additionally cona tacting such conveyed solids with other lim-tions exothermic reaction o! a solid path, the portions being controlled in amount to limit the temperatures attained subsequent to said additions, the total amount of liquid added being regulated to be only suiilciently in excess of the theoretical amount necessary to completely react the solid, to absorb only that amount of the heat of reaction to maintain the temperature oi the reacting products substantially above the vaporizing temperature of the liquid;

, continuously discharging the generated gas from k.said reaction chamber at predetermined points in said path; and continuously discharging the substantially dry residue from said reaction chamber 3. A process, for the continuous and simultaneous production of acetylene and substantially dry calcium hydrate by the reaction of calcium carbide and water, which comprises continuously introducing such carbide into a reaction chamber; contacting such carbide with a portion of such water so as to react a portion of such carbide; continuously conveying and agitating the unreacted carbide and the hydrate product of reaction along a predetermined path in said reaction chamber; contacting such conveyed carbide and hydrate with successive portions ofwater at predetermined points along its path of travel, the water being regulated in amount so as to produce a temperature of the generated acetylene substantially in excessA of 100 C. at said predetermined points and introduced directly into said carbide to prevent its contacting said acetylene: continuously discharging the generated acetylene from such reaction chamber at predetermined points in said path; and continuously discharging the substantially dry hydrate from said reaction lchamber at the end of said 1 path.

4.7A yprocess for the continuousand simultaneous production of a gas and a substantially dry residue by the exothermic reaction oi a solid and a liquid, which comprises continuously introducing said solid into a reaction chamber, contacting the solid in said reaction chamber with only suiiicient liquid, in excess of the theoretical amount necessary to completely react the solid, to absorb only that portion ofthe heat o! reaction necessary to maintain the products of reaction at a temperature substantially above the boiling point of said liquid, introducing said liquid directly into said solid to prevent its contacting the generated gas, continuously conveying kthe unreacted solid and the solid products of reaction along a predetermined path in said reaction chamber, and simultaneously agitating the unreacted solid'and solid products of reaction so as to completely reactthe solid, continuously discharging the generated gas from said chamber, and continuously discharging the substantially dry residue from said reaction chamber at the end point oi' said path.

5. A process for the continuous and simultaneous production of a gas and a substantially dry residue by the exothermic reaction of a solid and a liquid winch comprises continuously introducing said solid into a reaction chamber, contacting the said solid in the reaction chamber with only suilicient liquid in excess or the theoretical amount necessary to completely react the solid and to absorb only that portion of the heat of reaction necessary to maintain the products of reaction at a temperature substantially above the boiling point of said liquid, introducing said liquid directly into said solid to prevent its contacting the generated gas, continuously agitating the unreacted solid and the solid products of reaction so as to completely react the solid, removing at least av portion of the heat of reaction by contacting said products during said agitation withcooling surfaces to reduce the amount of said sagome@ water directly introduced, continuously discharging the generated gas from said chamber.

and continuously dry residu discharging the substantially e from the reaction chamber.

HUGO V. KOJOLA. MAURICE OBRIAN. 

